US4086160A - Treatment of solids-liquid-gas mixtures - Google Patents

Treatment of solids-liquid-gas mixtures Download PDF

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Publication number
US4086160A
US4086160A US05/703,663 US70366376A US4086160A US 4086160 A US4086160 A US 4086160A US 70366376 A US70366376 A US 70366376A US 4086160 A US4086160 A US 4086160A
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mixture
riser
downcomer
solids
chamber
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Expired - Lifetime
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US05/703,663
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English (en)
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Frank Cornelius Roesler
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Imperial Chemical Industries Ltd
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Imperial Chemical Industries Ltd
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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/24—Treatment of water, waste water, or sewage by flotation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1412—Flotation machines with baffles, e.g. at the wall for redirecting settling solids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/1462—Discharge mechanisms for the froth
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/1468—Discharge mechanisms for the sediments
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/1443—Feed or discharge mechanisms for flotation tanks
    • B03D1/1475—Flotation tanks having means for discharging the pulp, e.g. as a bleed stream
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/24—Pneumatic
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D1/00—Flotation
    • B03D1/14—Flotation machines
    • B03D1/24—Pneumatic
    • B03D1/26—Air lift machines
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B03—SEPARATION OF SOLID MATERIALS USING LIQUIDS OR USING PNEUMATIC TABLES OR JIGS; MAGNETIC OR ELECTROSTATIC SEPARATION OF SOLID MATERIALS FROM SOLID MATERIALS OR FLUIDS; SEPARATION BY HIGH-VOLTAGE ELECTRIC FIELDS
    • B03D—FLOTATION; DIFFERENTIAL SEDIMENTATION
    • B03D3/00—Differential sedimentation

Definitions

  • This invention relates to a method and apparatus (of the kind hereinafter defined) for the treatment of solids/liquid mixtures to effect separation by flotation and/or sedimentation and possibly also recycling of solids.
  • the method for the treatment of solids/liquid mixtures is of the kind wherein in a circulatory system having one or more chambers the mixture flows downwardly in one part and upwardly in another part a gas is supplied to and at least partly dissolved in the mixture, preferably during its downward flow, and a portion of the mixture, preferably during its upward flow, passes into a chamber in which separation of solids from the liquid in the mixture occurs by flotation and/or by sedimentation.
  • the apparatus for the treatment of solids-liquid mixtures is of the kind that comprises a circulatory system having one or more chambers, means for circulating a solids-liquid mixture downwardly in one part and upwardly in another part thereof, means for supplying a gas to the mixture, preferably during downward flow, and a separation chamber connected thereto in a manner such that a portion of the mixture, preferably during upward flow, passes into the separation chamber and undergoes separation of solids from the liquid.
  • Such a method and apparatus are particularly applicable to treatment of waste water, which term is to be understood to include water carrying any type of biologically degradable domestic and industrial waste materials for example normal domestic waste and the effluents produced by farms, food factories and other industries.
  • the methods generally employed in the treatment of waste water comprise a primary treatment by physical methods followed by a secondary treatment by biological methods.
  • the present invention relates to the secondary treatment stage.
  • the waste water is aerated and thereafter partial or total separation of sludge solids from liquid is performed. From the separation step part at least of the separated solids is usually returned to the aeration step so as to maintain the concentration of active solids and for further treatment.
  • the return of the separated solids to the aeration stage is achieved using mechanical pumps, at least two of which are required when separation is by both flotation and sedimentation, and thus risks of breakdown and costs of regular maintenance are incurred.
  • a method of treating a solids/liquid mixture in a circulatory system in part of which it flows downward and in another part of which it flows upwards in which a gas is supplied to and at least partly dissolved in the mixture and a portion of the mixture is diverted into a chamber in which solids are separated therefrom by flotation and/or sedimentation, characterised in that mixture relatively rich in solid is fed into the system hydrostatically.
  • the gas (which is normally air for aerobic treatments) is supplied to the mixture preferably at least partly during its downward flow.
  • gas supply in the riser is required at start-up, in order to set up circulation, it can be substantially or wholly shut off during steady operation.
  • the diverted mixture is driven into the separation chamber preferably by the hydrostatic pressure difference between the diverted and the undiverted mixture in the circulatory system. Since the mixture in upper parts of the circulatory system contains many bubbles but that in the separation chamber contains few, its density if lower than that of the separation chamber mixture, and consequently the mixture level in the circulatory system should be appropriately higher than that in the separation chamber. This is discussed in more detail below.
  • the mixture relatively rich in solids contains few bubbles and has a higher density than that of the mixture in these parts of the circulatory system in which by the design of the flow path bubbles are present.
  • this density difference is made use of by feeding the relatively rich mixture to the system at a lower level than that at which diverted mixture is taken off.
  • This mode of operation is especially suitable for recycling separated solids from the chamber to the circulation system.
  • the diverted portion of the mixture is preferably taken off during upward flow which then by the diversion is directed downwardly, and is caused to flow at a velocity less than that of the rising velocity of the gas bubbles at the take-off level. Means for doing this is described further below.
  • apparatus for treating a solids/liquid mixture comprising a circulatory system having one or more chambers, means for circulating solids/liquid mixture downwardly in one part of the system and upwardly in another part thereof, means for supplying a gas to the mixture, a separation chamber connected to the system to receive a portion of the mixture and means to return or feed to the system a mixture relatively rich in solids, the return or feed point being so disposed in the system that the relatively rich mixture is driven into it by means of hydrostatic pressure.
  • the separation chamber includes off-takes for purified liquid (that is, depleted in solid), sedimentation-enriched mixture and flotation-enriched mixture.
  • purified liquid that is, depleted in solid
  • sedimentation-enriched mixture Preferably both enriched mixtures therein separated are returned via the rich mixture feed point.
  • Preferred apparatus of the present invention includes means for providing the preferred features of the method of the invention.
  • the method and apparatus are suitable for the use in conjunction with the invention described and claimed in our co-pending UK Application No. 14142/75 (New Zealand application 180494), namely a method for solids-liquid separation wherein a solids-liquid mixture is circulated around a circulatory system comprising at least two substantially vertical ducts communicating with each other at their upper and lower ends such that it flows downwardly in one part of the system and upwardly in another part of the system, a gas being supplied to and at least partly dissolved in the mixture, preferably in the downwardly flowing mixture, and a portion of the upwardly flowing mixture containing dissolved gas passing into a flotation chamber connected to the circulatory system, in which flotation chamber the hydrostatic pressure gradually decreases as the mixture flows upwards and consequently gas is released from solution and forms gas bubbles attached to solid particles present in the mixture which carry the solid particles to the top of the liquid in the mixture; preferably the solid particles carried to the top of the liquid and the
  • an apparatus for solids-liquid separation comprising a circulatory system with a flotation chamber connected thereto, the circulatory system comprising at least two substantially vertical ducts communicating with each other at their upper and lower ends means for circulating a solids-liquid mixture around the system so that it flows downwardly in one part of the system and upwardly in another part of the system and means for supplying a gas to the mixture, preferably to the downwardly circulating mixture in the system, the flotation chamber being connected to the system in a manner such that a portion of the upwardly flowing mixture containing dissolved gas in the system passes into the flotation chamber and flows upwardly therein; preferably said flotation chamber is provided with means for removing solid particles from the top of the liquid therein and means for withdrawing clarified liquid.
  • the separation chamber is suitable connected to the riser and a portion of the solids-liquid mixture such as waste water flowing up the riser passes into the separation chamber.
  • FIG. 4 shows a main pipe 21, containing upwardly flowing solids-liquid mixture in which gas bubbles are present, and a side loop 22 connected to the main pipe through openings 23 and 24. Solids-liquid mixture enters side loop 22 through upper opening 23 and returns to the main pipe through lower opening 24 which is narrower than upper opening 23.
  • H effective hydrostatic head difference between 24 and 23.
  • h Geometrical height difference between 24 and 23.
  • E mean voidage fraction in main pipe 21 between 24 and 23.
  • A area of opening 24.
  • u Velocity of flow through opening 24.
  • u ⁇ 2 g H (neglecting friction in loop 22 and assuming that opening 24 is narrower than opening 23, so that u is large compared with w).
  • the flow of the mixture in the conduit leading to the separation chamber is designed to be less than the flow that would exceed in velocity the bubble rising velocity in the systen, at the level at which mixture passes from the system downwardly into the conduit leading to the separation chamber.
  • the separation chamber is a flotation chamber as described in co-pending UK Application No. 14142/75 with means for recycling separated solids.
  • This chamber is preferably located for the greater part of its length inside or adjacent to the riser of the apparatus of co-pending cognated UK Applications Nos. 23328/73 and 53921/73.
  • Solids-liquid mixture preferably enters the flotation chamber at or near its lower end, suitably through a plurality of openings each equipped with a trap or traps to prevent stray gas bubbles from entering the flotation chamber.
  • the upper part of the flotation chamber preferably widens to form a flotation basin. Floated solids rise to the top of the clarified liquid in this basin whilst the sinking solids which remain go to the bottom.
  • conduits are provided to return the floated and preferably also the sinking solids to the circulatory system.
  • the floated and sinking solids may enter the system separately but preferably the conduits bearing them are joined outside the system and all returned solids enter the system at the same level.
  • the conduit carrying the solids may for convenience be a pipe suspended in the riser.
  • the returned solids re-enter the system at a level sufficiently below that at which the solids-liquid mixture leaves the system for the hydrostatic head difference H to achieve the desired rate of recirculation of solids.
  • the velocity of liquid flow into the conduit leading to the separation chamber is suitably not greater than 10cm sec -1 , preferably less than 5cm sec -1 .
  • the velocity of not above 10cm sec -1 when a suitable trap and louvre means is used, ensures that no bubbles larger than 1mm diameter enter the separation chamber.
  • the voidage in the mixture in the riser is suitably 5 - 25% v/v, preferably 10 - 20% v/v.
  • the velocity of upward flow of liquid in the flotation chamber is suitably not more than 0.3m sec -1 , especially not more than 0.1m.
  • the residence time of the ascending mixture therein is on average at least 60 seconds and can exceed 400 seconds, for example 1000 seconds or more.
  • the depth of the riser and downcomer chambers is suitably at least 40m below the liquid level at the top of the circulatory system, that is in the gas disengagement basin (item 1 in the drawings). Preferable depth depends on the treatment duty (as measured by the required rate of oxygen transfer) and strongly on the shaft size (diameter), which determinds hydraulic friction. Suitably depths for shafts 2m to 3m diameter are at least 80m, and for very large shafts (greater than 5m diameter) 150 - 250m.
  • the ratio of the cross-sectional area of the separation chamber to that of the riser depends on the treatment time required in the circulatory system; in general it may be in the range 0.01 to 2.0, but will normally be in the range 0.25 to 2.0 for readily degradable effluents.
  • the invention provides a means whereby in waste water treatment airlift pumping may be used to carry out the auxiliary duty of moving liquor and/or sludge to and from flotation and sedimentation basins. This is achieved by tapping the flow in the circulatory system at two or more different levels so that the voidage in the system multiplied by the level difference supplies the driving head.
  • the use of mechanical pumps with their attendant difficulties is avoided.
  • FIG. 1 is a diagram of one form of the apparatus.
  • FIG. 2 is a diagram of more compact form of the apparatus, a portion only being shown comprising the upper part of the riser and associated flotation and sedimentation recycle sections.
  • FIG. 3 is a diagram of a simple form of trap to prevent large bubbles of gas from entering the flotation chamber. Such a trap may be used in the apparatus of FIGS. 1 and 2.
  • FIG. 4 is a diagram explaining the principle underlying the present invention.
  • the apparatus shown in FIG. 1 has a gas disengagement basin 1, into which a waste water conduit (not shown) feeds, with a deep shaft extending below it and containing downcomer 2 and riser 3 defined by partition 4.
  • Downcomer 2 and riser 3 communicate with each other at their upper ends in disengagement basin 1 and at their lower ends through opening 5 below the lower end of partition 4.
  • Oxygen-containing gas may be injected into downcomer 2 and riser 3 through spargers 6 and 7 respectively.
  • Towards its upper end riser 3 is divided to form a separation chamber 8 located within the riser but separated from disengagement basin 1 by-partition 9. Chamber 8 communicates with riser 3 through a plurality of circular openings which together form trap 10.
  • chamber 8 forms separation basin 11 situated alongside but at a lower level than disengagement basin 1. From basin 11 sinking sludge return pipe 12 and floated sludge return pipe 13 lead into riser 3 through openings 14 and 15 in the wall thereof below the lower end of chamber 8. Also from basin 11 liquor take-off pipe 16 connects with later stages in the treatment system.
  • the apparatus shown in FIG. 2 differs from that shown in FIG. 1 in the detailed construction of the sludge recycle system.
  • separation chamber 8 is located for a major part of its length approximately centrally within riser 3 instead of to one side.
  • Sinking solids return pipe 12 and floated solids return pipe 13 join one another outside riser 3 and the resulting joint solids return pipe 17 is suspended in the riser having entered it through opening 18 in its outer wall.
  • Return pipe 17 has upward extension 21 to facilitate access for removal of any blockage that may occur.
  • Ths construction is more compact than that of FIG. 1 and entails less digging during its installation, if the shaft is beneath ground level.
  • the trap shown in FIG. 3 comprises three rows of circular holes 19, each row having associated with it a skirt 20. With this trap built onto separation chamber 8, if the flow of liquid from riser 3 through holes 19 is relatively slow, bubbles in the liquid flowing up the riser will sweep past the trap and fail to enter chamber 8.
  • start-up is achieved by injecting air from a compressor into riser 3 through sparger 7. This causes the upper part of riser 3 to operate as an air-lift pump and waste water begins to circulate around the apparatus in the direction shown by the arrows in FIG. 1.
  • the flow rate reaches a predetermined minimum value the injection of air into the downcomer 2 through sparger 6 is commenced and gradually increased. Preferably this is done in stages.
  • all or most of the air is injected into downcomer 2.
  • FIG. 1 Referring to the discussion of the operation of the system earlier in this specification, in FIG. 1:
  • A sum of the areas of openings 14 and 15
  • H 1 hydrostatic head difference between trap 10 and opening 14 (sinking solids)
  • H 2 hydrostatic head difference between trap 10 and opening 15 (floated solids)
  • H hydrostatic head difference between trap 10 and the bottom of return pipe 17.

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  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Biotechnology (AREA)
  • Hydrology & Water Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Physical Water Treatments (AREA)
  • Devices And Processes Conducted In The Presence Of Fluids And Solid Particles (AREA)
  • Aeration Devices For Treatment Of Activated Polluted Sludge (AREA)
  • Biological Treatment Of Waste Water (AREA)
  • Processing Of Solid Wastes (AREA)
US05/703,663 1975-07-10 1976-07-08 Treatment of solids-liquid-gas mixtures Expired - Lifetime US4086160A (en)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
UK29058/75 1975-07-10
GB29058/75A GB1540065A (en) 1975-07-10 1975-07-10 Aerobic biological treatment of wastewater

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US (1) US4086160A (ko)
JP (1) JPS5222167A (ko)
AU (1) AU503527B2 (ko)
CA (1) CA1060589A (ko)
DE (1) DE2631068A1 (ko)
FR (1) FR2317014A1 (ko)
GB (1) GB1540065A (ko)
ZA (1) ZA764072B (ko)

Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4251361A (en) * 1979-11-13 1981-02-17 Conoco, Inc. Hybrid gas flotation separator
US4272379A (en) * 1979-10-26 1981-06-09 C-I-L Inc. Method for protecting a bioreactor pressurized head tank against extreme surges of influent waste water
US4272375A (en) * 1979-10-26 1981-06-09 C-I-L Inc. Long vertical shaft bioreactor of simplified design
US4279754A (en) * 1979-10-26 1981-07-21 C-I-L Inc. Means for separation of gas and solids from waste mixed liquor
US4297217A (en) * 1979-05-23 1981-10-27 Imperial Chemical Industries Limited Treatment of wastewater
US4304665A (en) * 1979-01-15 1981-12-08 Imperial Chemical Industries Limited Process for treatment of wastewater
US4306969A (en) * 1979-07-16 1981-12-22 Industrial Research Institute Apparatus for sewage purification
US4340484A (en) * 1979-10-26 1982-07-20 C-I-L Inc. Method for the froth flotation separation and treatment of slowly biodegradable components in waste treatment
US4341632A (en) * 1977-12-23 1982-07-27 Linde Aktiengesellschaft Destruction of bulking sludge
US4367146A (en) * 1979-10-26 1983-01-04 C-I-L Inc. Long vertical shaft bioreactor with modified waste liquor injection
US4374027A (en) * 1978-02-06 1983-02-15 International Telephone And Telegraph Corporation Process for the secondary treatment of wastewater
US4374730A (en) * 1980-01-25 1983-02-22 Basf Aktiengesellschaft Process and apparatus for the biological purification of sewage
US5643459A (en) * 1995-04-26 1997-07-01 Cominco Engineering Services Ltd. Flotation method and apparatus
US5645726A (en) * 1996-03-14 1997-07-08 Deep Shaft Technology Inc. Treatment of waste liquor in a vertical shaft bioreactor
US5650070A (en) * 1996-03-14 1997-07-22 Deep Shaft Technology Inc. Aerobic long vertical shaft bioreactors
US5660724A (en) * 1996-05-28 1997-08-26 Deep Shaft Technology Inc. Multi-pressure head tank for use with vertical shaft bioreactors
US5690834A (en) * 1994-04-11 1997-11-25 Hoechst Aktiengesellschaft Process and apparatus for separating off suspended matter from liquids
US6337023B1 (en) 2000-09-01 2002-01-08 Paul C. Broussard, Sr. Flotation apparatus for clarifying produced water
CN113349396A (zh) * 2021-06-11 2021-09-07 万元坤 一种用于歺饮垃圾清杂提纯加工饲料的处理系统

Families Citing this family (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JPH04607Y2 (ko) * 1985-03-29 1992-01-09
JP4437436B2 (ja) * 2003-12-22 2010-03-24 株式会社日本触媒 分離装置、それを備えた分離システム及び分離装置の使用方法

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US1357587A (en) * 1919-12-01 1920-11-02 Dorr Co Method of and apparatus for treating waste liquors
US3374893A (en) * 1966-12-06 1968-03-26 G D Peters & Co Engineering Lt Sewage purification plant
US3422007A (en) * 1965-10-22 1969-01-14 Francis J Larkin Waste treatment process
US3476682A (en) * 1966-05-09 1969-11-04 Wibau Gmbh Method and apparatus for the purification of sewage
US3945916A (en) * 1973-06-25 1976-03-23 L Air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Purification of effluent

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US1341770A (en) * 1915-07-26 1920-06-01 William W Wilson Apparatus for mineral separation
DE2050635C3 (de) * 1970-10-15 1983-11-10 Otto Dürr Anlagenbau GmbH, 7000 Stuttgart Verfahren und Vorrichtung zum Trennen von Lack und Abwasser

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US1357587A (en) * 1919-12-01 1920-11-02 Dorr Co Method of and apparatus for treating waste liquors
US3422007A (en) * 1965-10-22 1969-01-14 Francis J Larkin Waste treatment process
US3476682A (en) * 1966-05-09 1969-11-04 Wibau Gmbh Method and apparatus for the purification of sewage
US3374893A (en) * 1966-12-06 1968-03-26 G D Peters & Co Engineering Lt Sewage purification plant
US3945916A (en) * 1973-06-25 1976-03-23 L Air Liquide, Societe Anonyme Pour L'etude Et L'exploitation Des Procedes Georges Claude Purification of effluent

Non-Patent Citations (1)

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Title
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Cited By (19)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4341632A (en) * 1977-12-23 1982-07-27 Linde Aktiengesellschaft Destruction of bulking sludge
US4374027A (en) * 1978-02-06 1983-02-15 International Telephone And Telegraph Corporation Process for the secondary treatment of wastewater
US4304665A (en) * 1979-01-15 1981-12-08 Imperial Chemical Industries Limited Process for treatment of wastewater
US4297217A (en) * 1979-05-23 1981-10-27 Imperial Chemical Industries Limited Treatment of wastewater
US4306969A (en) * 1979-07-16 1981-12-22 Industrial Research Institute Apparatus for sewage purification
US4272379A (en) * 1979-10-26 1981-06-09 C-I-L Inc. Method for protecting a bioreactor pressurized head tank against extreme surges of influent waste water
US4340484A (en) * 1979-10-26 1982-07-20 C-I-L Inc. Method for the froth flotation separation and treatment of slowly biodegradable components in waste treatment
US4272375A (en) * 1979-10-26 1981-06-09 C-I-L Inc. Long vertical shaft bioreactor of simplified design
US4367146A (en) * 1979-10-26 1983-01-04 C-I-L Inc. Long vertical shaft bioreactor with modified waste liquor injection
US4279754A (en) * 1979-10-26 1981-07-21 C-I-L Inc. Means for separation of gas and solids from waste mixed liquor
US4251361A (en) * 1979-11-13 1981-02-17 Conoco, Inc. Hybrid gas flotation separator
US4374730A (en) * 1980-01-25 1983-02-22 Basf Aktiengesellschaft Process and apparatus for the biological purification of sewage
US5690834A (en) * 1994-04-11 1997-11-25 Hoechst Aktiengesellschaft Process and apparatus for separating off suspended matter from liquids
US5643459A (en) * 1995-04-26 1997-07-01 Cominco Engineering Services Ltd. Flotation method and apparatus
US5650070A (en) * 1996-03-14 1997-07-22 Deep Shaft Technology Inc. Aerobic long vertical shaft bioreactors
US5645726A (en) * 1996-03-14 1997-07-08 Deep Shaft Technology Inc. Treatment of waste liquor in a vertical shaft bioreactor
US5660724A (en) * 1996-05-28 1997-08-26 Deep Shaft Technology Inc. Multi-pressure head tank for use with vertical shaft bioreactors
US6337023B1 (en) 2000-09-01 2002-01-08 Paul C. Broussard, Sr. Flotation apparatus for clarifying produced water
CN113349396A (zh) * 2021-06-11 2021-09-07 万元坤 一种用于歺饮垃圾清杂提纯加工饲料的处理系统

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Publication number Publication date
DE2631068A1 (de) 1977-01-27
ZA764072B (en) 1977-06-29
FR2317014A1 (fr) 1977-02-04
FR2317014B1 (ko) 1980-05-30
JPS5222167A (en) 1977-02-19
AU1583476A (en) 1978-01-19
GB1540065A (en) 1979-02-07
JPS6143120B2 (ko) 1986-09-25
CA1060589A (en) 1979-08-14
AU503527B2 (en) 1979-09-06

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